Heat exchanger

ABSTRACT

Disclosed is a shell-and-tube heat exchanger type with a tube bundle and has a redistribution chamber connected to tubes of the tube bundle and to a duct. The duct extends between the redistribution chamber and the shell.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation of U.S. Ser. No. 16/469,129 filed 12Jun. 2019, and now U.S. Pat. No. 10,857,480 issued 8 Dec. 2020, which isthe U.S. national phase of PCT application PCT/NL2018/050711 filed 26Oct. 2018, which claims benefit of European patent application No.17198990.8 filed 27 Oct. 2017. The contents of the above patentapplications are incorporated by reference herein in their entirety.

INTRODUCTION

The invention pertains to a high pressure carbamate condenser. Thecondenser comprises a shell-and-tube heat exchanger which comprises atube bundle mounted in a shell. The high pressure carbamate condensercan in particular be used for condensing carbamate in urea productionplants of the stripping type. In some embodiments, corrosive solutionscomprising carbamate are present in operation at both the shell side andthe tube side, in particular both inside at least some tubes of the tubebundle and in the space between the tubes.

A commonly used type of carbamate condenser is the pool condenserdescribed in “A lower cost design for urea”, Nitrogen no. 222,July-August 1996, page 29-31. Such a pool condenser comprises a tubesheet. Tube sheets are more generally a typical part of high pressurecarbamate condensers of the shell-and-tube heat exchanger type. The tubesheet is typically a planar metal plate delimiting the shell space inthe condenser from a header. The tube sheet furthermore seals off oneend of the typically cylindrical shell. The tube sheet is provided withnumerous bore holes. The tubes are inserted through the bore holes orare joined to the tube sheet aligned with the holes, such that fluid canflow between a header and the tubes. The tube bundle often has a verylarge number of tubes, e.g. more than 100 tubes or even more than 1000tubes. The header is used for distributing fluid from an inlet to aplurality of tubes, or for collecting fluid from a plurality of tubes toan outlet.

In known carbamate condensers, the tube sheet generally needs to be ableto withstand high pressure. Furthermore, preventing corrosion is achallenge because carbamate is highly corrosive, especially at the hightemperatures of high pressure carbamate condensation. To achieve highmechanical strength and high corrosion resistance, known tube sheets arefrequently made from carbon steel lined with a layer of highly corrosionresistant steel such as duplex stainless steel alloys on the side (orsides) exposed to corrosive medium. This increases construction costs,for example because of the difficult welding of the tubes to the tubesheet.

A known tube sheet for a kettle type carbamate condenser in a urea plantis illustrated in EP 0464307 and in U.S. Pat. No. 4,082,797.

The construction of the tube sheet is generally challenging andexpensive. The present invention generally addresses disadvantages ofknown high pressure carbamate condensers with tube sheets, such as thehigh construction costs associated with the tube sheet.

SUMMARY

The present disclosure relates in a first aspect to a shell-and-tubeheat exchanger which comprises a vessel which comprises a shell and atleast one tube bundle, wherein the shell encloses a vessel space,wherein the tube bundle comprises tubes having ends, and wherein a shellspace is provided between the tubes and the shell, wherein the heatexchanger further comprises a redistribution chamber located in saidvessel space, wherein said redistribution chamber comprises a wall forseparating a first fluid in the shell space from a second fluid insidethe redistribution chamber, wherein a plurality of said tubes areconnected to a single redistribution chamber such that said second fluidcan flow between said tubes and said redistribution chamber, wherein thecondenser further comprises a duct extending from an opening for thesecond fluid in said shell through said vessel space to saidredistribution chamber, such that the second fluid can flow between atube end and said opening for the second fluid in said shell throughsaid redistribution chamber and said duct.

The invention also pertains to a urea production plant comprising a highpressure urea synthesis section comprising a reactor, a stripper and ahigh pressure carbamate condenser, wherein the high pressure carbamatecondenser is as described, and wherein optionally the reactor and thehigh pressure carbamate condenser are combined in a single vessel whichvessel has a liquid outlet connected to the stripper.

The invention further pertains to a urea production process wherein ureais formed in a reactor to give urea synthesis solution, at least a partof said urea synthesis solution is stripped in a stripper to givestripped urea solution, and wherein gas from the stripper is condensedin a high pressure carbamate condenser, wherein the process is carriedout in a plant as described and/or wherein the high pressure carbamatecondenser is as described.

More generally, the invention also pertains to a shell-and-tube heatexchanger comprising such a vessel and comprising such a shell, tubebundle, redistribution chamber and duct. The shell-and-tube heatexchanger is e.g. configured for condensation of compounds other thancarbamate, and/or for operation at pressures below 100 bar, and/or forheat exchange processes other than condensation. The heat exchanger canbe used in urea production and in other plants and processes.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 illustrates a reference carbamate condenser with a tube sheet.

FIGS. 2A-2D illustrate examples of a high pressure carbamate condenser.

FIG. 3 schematically illustrates an example of a urea plant.

DETAILED DESCRIPTION

In this application, for process streams (i.e. not for steam lines),high pressure (HP) is above 100 bar, for instance 120 to 300 bar,typically 150 to 200 bar. Medium pressure (MP) is for example 10 to 70bar (including intermediate pressure of 30 to 70 bar), in particular 15to 25 bar, and low pressure (LP) is for example 0 to 10 bar, inparticular 1 to 8 bar or 2 to 5 bar. As used herein, “carbamate” refersto ammonium carbamate.

The high pressure carbamate condenser is preferably a submergedcondenser, as opposed to a falling film condenser. In operation of asubmerged condenser, the condensation is carried out in a space withliquid as the continuous phase and with the gas to be condenseddispersed in the liquid. A liquid level is hence present in thecondensation space. For example, the tubes are covered by the condensedliquid in operation (on the inside or on the outside of tubes), andpreferably the tubes are submerged in the condensed liquid. Thesubmerged condenser comprising a shell-and-tube heat exchanger isconfigured for condensation inside the tubes or in the shell space.Suitably, the condensation is carried out in the shell space. The shellspace is the empty space to which the outer surface of the tubes isexposed. The shell space is confined by the shell. Condensation in theshell space is one option for providing a relatively simple constructionwherein the condensate has sufficient residence time in the condenser.This allows advantageously for a part of the urea to be formed alreadyin the condenser. A longer residence time can also be provided in caseof condensation in the tubes by using more tubes and/or tubes with alarger diameter.

The condenser is e.g. a high pressure carbamate condenser configured assubmerged condenser with condensation carried out in the shell space,for example based on the pool condenser design, but modified to have oneor more such said redistribution chambers and ducts. An example poolcondenser design is illustrated in Nitrogen No. 222, July-August 1996,pages 29-31. Preferably, cooling fluid is provided in the tubes. In thepresent invention, the cooling fluid is e.g. a process stream, such as asolution comprising urea and carbamate, which solution is heated whenpassing through the tubes, optionally water (process condensate) is inaddition used as cooling fluid.

The high pressure carbamate condenser has for instance a verticalconfiguration, with (the straight part of) the tubes in verticalarrangement with respect to gravity, when installed in the urea plant.Generally, the vertical carbamate condenser is configured forcondensation in the shell space or in the tubes, preferably in the shellspace. The condenser has e.g. a U-shaped or straight tube bundle,preferably a U-shaped tube bundle. For instance a vertical carbamatecondenser that is of the type described in U.S. Pat. No. 6,518,457and/or which has a tube bundle with tube ends at the bottom can bemodified with redistribution chambers and ducts according to the presentinvention. Furthermore a vertical condenser with a tube bundle with tubeends at the top can be provided with redistribution chambers and ductsaccording to the invention, these are e.g. placed at the top of thecondenser.

The high pressure carbamate condenser preferably has a horizontalconfiguration, with (the straight part of) the tubes in horizontalarrangement with respect to gravity, when installed in the urea plant.For example, the high pressure carbamate condenser with horizontalorientation can be configured for condensation in the tubes and forreceiving cooling fluid in the shell space. For instance a kettle typecarbamate condenser, e.g. as described in EP 0464307 or U.S. Pat. No.4,899,813, can be modified with a redistribution chamber and duct asdescribed herein.

In an embodiment the condenser is configured as a horizontal submergedcondenser. This advantageously allows for lower height of the plant. Ina preferred embodiment, the condenser is configured as a horizontalsubmerged condenser operated with the condensation on the shell side(i.e. in the shell space). This provides the further advantage that thecondenser volume can be easily designed for a longer residence time ofthe condensate. This may also be used to create a pool reactor. Thecondensation on the shell side also leads to having the high pressuremedium on the shell side which makes the condenser easier to manufactureand in particular allows for a simpler design of the redistributionchamber.

Hence, in a preferred embodiment, the vessel comprises a gas inlet tothe shell space, for gas to be condensed. The gas inlet comprises anopening in the shell. The gas inlet allows for operation withcondensation in the shell space and cooling fluid(s) in the tubes. Thevessel furthermore comprises an outlet for liquid from the shell space,such as for a carbamate-containing liquid stream. The outlet comprisesan opening in the shell. The vessel preferably comprises a gasdistributor connected to the gas inlet. The gas distributor preferablycomprises a plurality of passageways for gas from the gas inlet into theshell space. The gas distributor can be used for distributing gas to becondensed over and into the shell space, in particular into the liquidin operation. The gas distributor is preferably arranged below theliquid level in operation. The gas distributor for instance comprises asparger with one or more tubes extending in the length of the vessel,said tube provides with arms extending in the width of the vessel atboth sides of said tubes, wherein the arms have numerous openings forgas (e.g. more than 50 openings per arm) at the upper side of the arms.Gas to be condensed is e.g. a mixture comprising CO₂ and NH₃ from a highpressure stripper. The vessel furthermore preferably comprises a liquidinlet to the shell space, for introducing into the shell space a liquidstream comprising ammonia and/or carbamate recycle stream. In an exampleembodiment, a carbamate recycle stream, e.g. from a medium pressuresection of a urea plant, is introduced into the shell space through anopening in the shell at the top of the shell. This can provide forimproved mixing because the carbamate recycle liquid has a higherdensity than the condensing mixture in the shell space. The opening inthe shell for carbamate recycle is preferably in length direction spacedless than 1 m from a redistribution chamber. This provides for goodmixing of fluids in the shell space near the redistribution chamber.

The carbamate condenser has e.g. a horizontal or vertical arrangement.In case of a horizontal carbamate condenser with a gas distributor, thegas distributor extends horizontal and in parallel with (the straightparts of) the tubes, so as to introduce gas to be condensed in the shellspace at various outlets of the gas distributor which are spaced apartin horizontal direction. In this embodiment, the length direction isalso horizontal. The tubes are preferably U-shaped.

The condenser preferably comprises a liquid distributor for distributingliquid into the shell space at a plurality of openings. These openingsare preferably spaced apart in the length direction of the condenser.The liquid distributer is e.g. connected to an ammonia supply member,such as with a liquid flow connection to a compressor for ammonia feed.Typically the liquid distributor (e.g. ammonia distributor) is connectedto an opening in the shell, and is in operation for instance submergedin liquid present in the shell space.

A tube bundle generally comprises a plurality of tubes, wherein thetubes comprise or consist of straight tube parts. Typically the straightparts of the tubes are arranged in parallel and are spaced apart fromeach other. As used in this application, if condensation is carried outin the shell, the tubes of a single tube bundle comprise the samecooling fluid. Accordingly, a redistribution chamber is preferablyconnected to tubes of a single tube bundle. In a further embodiment twoor more cooling fluids are used in the tubes (with separate supplymembers), and the condenser contains a plurality of tube bundles. Thetube bundles can be combined in a combined tube bundle. The straightparts of all tubes in a combined tube bundle are preferably parallel toeach other.

In order to have sufficient heat exchange surface, the high pressurecarbamate condenser has one or more tube bundles with for instance atleast 300 tubes in the bundles in total, typically 1000 to 4000, such as1500 to 3000 tubes in total, with e.g. at least 100 tubes in each tubebundle. Tubes have for instance constant internal diameter over theirlength. Preferably, each redistribution chamber is connected to onlyinlet ends or only outlet ends of a single tube bundle.

In some embodiments, the tube bundle comprises straight tubes with tubeends at opposed sides of the tube bundle in the length direction.Redistribution chambers can be provided at each end of the tube bundle.In principle, also a tube sheet can be used at one end and aredistribution chamber at an opposed end. The tube bundle can be locatedat any position in the length of the vessel, e.g. at an end or in thecenter of the vessel. The straight part of the tubes have for instance alength of 20-90% of the length of the vessel, e.g. preferably at least30%, at least 40%, at least 50%, or at least 60%, and/or e.g. up to 90%,up to 80%, or up to 70% of the length of the vessel. In someembodiments, the straight parts of the tubes have a length of 60 to 90%of the length of the vessel, and preferably the condensate obtained bycondensation in the condenser is supplied to a high pressure reactor. Insome embodiment, the straight parts of the tubes have a length of 20 to60% of the length of the vessel, and preferably the condensate obtainedby condensation in the condenser is supplied to a high pressurestripper. For instance the condensate is supplied directly to thestripper such that the high pressure stripper receives condensate havingthe same composition as at the liquid at the outlet of the condenser. Ina urea plant according to such embodiment, the reactor and condenser arecombined in a single vessel.

In some embodiments, redistribution chambers are provided at both endsof the tubes (preferably of a straight tube bundle) and theredistribution chamber(s) are spaced apart from the vessel by adistance, in the length direction, of at least 1%, at least 5%, at least10%, or at least 20% at the length of the vessel, at one or both ends ofthe tube bundle. A larger spacing between the redistribution chamber andvessel, at one or both ends of the tube bundle, gives a relativelylarger shell space for condensate and may contribute to a largerresidence time of condensate in the shell space. This may allow for ureaformation to occur and e.g. for operation as pool reactor. The condensedcarbamate is typically sent to a urea reactor and is in some embodimentssent directly to the stripper in operation. Especially for larger tubelengths (based on the straight tube part), such as above 5 m, above 10m, above 20 m, or above 30 m, the manufacturing of straight tubes can besimpler than for U-shaped tubes.

In further embodiments, the tube bundle is a bundle of U-shaped tubes,wherein each tube comprises a bend and two legs, the legs being straighttube parts. The carbamate condenser optionally comprises a reactor partbetween the bend of the U-shaped tube bundle and the shell (opposite ofthe tube legs), for example but not exclusively in case of a poolreactor. An example pool reactor is described in U.S. Pat. No.5,767,313. The straight parts of the tubes of the U-shaped tube bundleare arranged in the length direction of the shell. In some embodiments,the shell comprises an essentially cylindrical middle part, having adiameter and a length, and with cap parts at both ends. In case of aU-shaped tube bundle, for instance a substantially hemispherical cap(optionally with a manhole) is joined to the end of the middle part thatis close to the bend of the tube-bundle of the tube bundle as well as atthe other end of the middle part. In the prior art, e.g. as in U.S. Pat.No. 5,767,313, a tube sheet is provided at end away from the bend of theU-shaped tube-bundle, to connect the tube ends with feed and drain linesthrough a header.

The invention is broadly based on the judicious insight to place aredistribution chamber inside the shell and to connect tubes of the tubebundle to the redistribution chamber, and to provide a duct connectingthe redistribution chamber with a feed or drain line through an openingin the shell. The duct is arranged inside the shell and allows theredistribution chamber to be spaced apart from the shell. The duct is inoperation at one side in contact with a cooling fluid and at the otherside with the gas to be condensed and/or the condensate formed in thecondenser. The same applies for the wall of the redistribution chamber.In embodiments with condensation on the shell side (outside the tubes),the shell is the equipment part that contains the high pressurecondensing medium and that is on the inside in contact with that medium.At outside the shell is typically exposed to ambient.

In a typical embodiment, every tube of the tube bundle has two tubeends, and for each tube one tube end is connected to an inletredistribution chamber (for distributing fluid to a plurality of tubes)and the other tube end to an outlet redistribution chamber (forcollecting fluid from a plurality of tubes).

In a preferred embodiment, the vessel comprises two tube bundles, forinstance for two different cooling fluids, each tube bundle with aninlet redistribution chamber and an outlet redistribution chamber, suchthat the vessel contains four redistribution chambers.

The redistribution chamber comprises a wall. The wall includes a wallpart with bore holes. In operation fluid flows between theredistribution chamber and the tubes connected to it through the boreholes. However, unlike a conventional tube sheet, this wall part, andmore particularly the entire redistribution chamber, is spaced apartfrom the shell. Hence, typically no part of the redistribution chamberis in direct contact with (the internal surface of) the shell.

The redistribution chamber is connected to tube ends. In particular thewall part with bore holes is connected to tube ends, for example withcrevice-free joints.

Accordingly, at least some tube ends are located inside the spaceenclosed by the shell (the vessel space) and are connected (for fluidflow) to an opening in the shell through a redistribution chamber and aduct extending between the redistribution chamber and the shell. Theredistribution chamber is spaced apart from that shell opening, e.g. byat least 5 cm, at least 10 cm or at least 40 cm. The redistributionchamber is also spaced apart, preferably entirely, from the shell,preferably by at least 5 cm, at least 10 cm or at least 40 cm. Thesespacing are preferably provided by empty space that in operation can befilled with cooling fluid or condensing medium. Support elements can bepresent between the redistribution chamber and the shell, as well as theducts.

Advantageously, in a preferred embodiment with cooling fluid(s) in thetubes, the high pressure is on the outside of the redistributionchamber, not on the inside.

Advantageously, the walls of the redistribution chamber can be lessthick than the known tube sheets, because of the smaller dimensions ofthe redistribution chamber compared to a tube sheet. In particular, theredistribution chamber has a smaller surface area in cross sectionperpendicular to the length of the vessel compared to the shell and to atube sheet sealing off the shell. This leads to significantly smallerforces (stresses) for which the redistribution chamber walls need to bedesigned.

In a preferred embodiment, a (plate) element with bore holes of theredistribution chamber (or common to a stack of redistribution chambers)has for instance only a relatively small flange around the tube bundles,such as less than 40 cm, less than 20 cm, or less than 10 cm around eachtube bundle at each side, from the outer tubes of each tube bundle.

The redistribution chamber can for instance be provided with an internalload-bearing structure, such as a spacer. The walls of theredistribution chamber can be made of, or consist of, a single sheet ofcorrosion resistant material, such as duplex stainless steel. The weldconnections of the tubes to the redistribution chamber are easier tomanufacture for the preferred embodiment with a single sheet wall,especially because there is no risk of carbon steel exposure.

Furthermore, advantageously the walls of the redistribution chambersalso contribute to the heat exchanging surface since in operation theycan be at one side in contact with cooling fluid and at the other sidewith condensing medium.

The invention also pertains to a urea production plant, comprising ahigh pressure urea synthesis section comprising the high pressurecarbamate condenser as described, a reactor and a stripper. The reactor,condenser and stripper each operate at high pressure. The stripper has agas flow line to the condenser, the condenser has a liquid flow line tothe reactor, and the reactor has a liquid flow line to the stripper forat least part of the urea solution. The reactor and condenser areoptionally combined in a single vessel, which is for instancehorizontally placed, and from which condensate is supplied directly to astripper. Such a single vessel e.g. comprises a condenser part and areactor part. Also in the case of a condenser and a reactor provided asseparate vessels (typically with a vertical reactor vessel) optionallyalready some urea is formed in the condenser. The plant for examplecomprises a gas flow line from the stripper to the shell space and aliquid flow line from the stripper to the tube bundle of the carbamatecondenser; or the plant for example comprises a gas flow line from thestripper to the tube bundle and a liquid flow line from the stripper tothe shell space of the carbamate condenser; wherein said flow line tothe tube bundle is through a duct and a redistribution chamber asdescribed.

In operation, the urea synthesis stream from the reactor comprisingurea, water, and CO₂ and NH₃ (in part as carbamate) is supplied at leastin part to the stripper. Carbamate is dissociated into CO₂ and NH₃ inthe stripper and a part of the unreacted components is removed from thesolution as gas. In the stripper, dissociation of carbamate is promotedby heating and counter-current contact with a strip gas to promotedissociation. The stripper uses heating and for instance a supply ofhigh pressure CO₂ as stripping agent, so-called thermal stripping isalso possible. The heating in the stripper is typically indirect heatexchange with steam, typically with steam on the shell side and the ureasynthesis stream in the tubes of a shell-and-tube heat exchanger used asstripper. Stripped urea solution, still containing some carbamate andNH₃, is typically expanded to a lower pressure and supplied to arecovery section wherein more carbamate is removed from the ureasolution; the recovery section includes e.g. MP recovery with LPrecovery section downstream in series, or only LP recovery. The mixedgas stream from the stripper containing NH₃ and CO₂ is supplied to thehigh pressure condenser, either to the tubes or to the shell space.

In a preferred embodiment, the mixed gas stream is supplied to the shellspace, through an opening in the shell. One or more cooling fluids aresupplied to the tubes, through a duct and a redistribution chamber asdescribed (with separate ducts and redistribution chambers for differentcooling fluids). Liquid condensate is formed and is in this preferredembodiment present in the shell space, with optionally gas at the toppart of the shell space. The condensed liquid is in contact with thetubes such that the condensate is typically subcooled.

In this preferred embodiment, a gas distributor, such as a sparger, isused to distribute the gas to be condensed in the shell space, inparticular for distribution in the length direction of the condenser.The sparger is e.g. a tube having an inlet connected to an inlet openingof the shell, optionally with arms, and having plurality of outletopenings for gas, wherein the outlet openings are spaced apart in thelength direction. The arms extend in the width of the vessel and haveopenings for gas. A preferred carbamate condenser comprises suchsparger. For horizontal condensers, both the gas distributor and thestraight parts of the tubes extend in parallel in the length direction;preferably at least a part of the gas distributor is arranged below thestraight parts. This advantageously provides for improved distributionof heat of condensation in the shell.

In some embodiments, ammonia is also introduced into the shell space,e.g. using a liquid distributor, especially if a CO₂ stripper is used.

In some embodiments, the heat of condensation is at least in partwithdrawn by producing steam (water vaporization) in at least some ofthe tubes in case of condensation in the shell space, and in the shellspace in case of condensation in the tubes, the steam is e.g. formedfrom process condensate.

The parts of the carbamate condenser that are in contact with processmedium, especially at higher temperature (for example the process mediumcondensing at high pressure in the condenser) are usually made fromcorrosion resistant materials, in particular urea grade steel, such asan austenitic-ferritic duplex stainless steel (duplex steel). Forinstance the shell is at the inside typically provided with overlaywelding (i.e. a weld overlay) or internal lining made of urea gradesteel or other corrosion resistant metal, e.g. duplexaustenitic-ferritic stainless steel, AISI 316L steel, or INOX 25/22/2Cr/Ni/Mo steel. Such internal lining is typical for the shell of a highpressure carbamate condenser. The outside shell is e.g. a carbon steelshell and is e.g. at least 30 mm or at least 40 mm thick.

In some embodiments, the HP carbamate condenser comprises two tubebundles. This can be used to implement a process wherein two differentcooling fluids are used, for instance a first tube bundle for producingsteam from water, and a second tube bundle wherein an aqueous solutioncomprising urea and carbamate is heated to cause dissociation ofcarbamate.

Such a condenser can for instance be used in a plant and process asdescribed in US 2015/0119603.

In an embodiment the HP condenser with two tube bundles is used in aurea production process wherein in a first tube bundle steam is producedfrom water (also referred to as condensate). In a second tube bundle asolution containing carbamate (and typically also urea) is heated by theheat of condensation received from the high pressure process medium onthe shell side, such that at least part of the carbamate in the solutionin the second tube bundle dissociates into NH₃ and CO₂. The solution isfor instance obtained as the stripped urea solution from the HPstripper, or as a part of the urea synthesis solution from the reactorthat is not stripped in the HP stripper. For example a urea solutionthat is a part of the liquid from the reactor (optionally, fromcombination vessel comprising the condenser and the reactor) and/or ureasolution that is at least a part of the liquid from the stripper, issupplied to the second tube bundle, in particular through the inletredistribution chamber and the inlet duct to the second tube bundle,optionally with intermediate steps such as expansion and gas/liquidseparation (flashing). For instance, all or a part of the urea solutionexiting the stripper is expanded, optionally flashed, and optionallyfurther expanded and supplied at medium pressure (e.g. 10-35 bar) to thesecond tube bundle.

In some embodiments, the second tube bundle receives a carbamatecontaining solution, for instance in urea production processes involvingsupplying a urea solution to the second tube bundle directly orindirectly from the reactor (or reactor part), e.g. from the reactor,the stripper, or from a recovery section, preferably through an inletduct and inlet redistribution chamber. In such embodiments thermaldissociation of carbamate (to CO₂ and NH₃ gas) can take place in thesecond tube bundle.

The high pressure condenser can for instance be used in a ureaproduction process of the stripping type, wherein a part of the ureasolution from the reactor is sent to a high pressure stripper, andanother part of the solution bypasses the stripper and is sent to amedium pressure treatment step involving dissociation of carbamate byheating the solution at medium pressure. The invention also pertains tosuch a process. An example of such a process, using a different typehigh pressure condenser, is described US 2004/0116743. In the operationof the high pressure carbamate condenser of the present invention, andin a preferred process of the invention, the medium pressure treatmentstep is for instance carried out by passing the urea solution throughthe (second) tube bundle of the high pressure carbamate condenser inindirect heat exchanging contact with condensing gases in the condenserthat are received from the stripper. In a further embodiment, thecarbamate condenser is used for raising steam (e.g. in a tube bundle),which steam is used for supplying heat to a medium pressure dissociationstep of urea solution obtained from the stripper or non-stripped ureasolution from the reactor.

For conventional HP carbamate condensers, a challenge in case of havingin operation carbamate containing liquid(s) in at least some of thetubes as well as in the shell space is the risk of corrosion, and themanner of tube to tube sheet connection, e.g. for the pool condenserwith a tube sheet as illustrated in US 2015/0119603. The presentinvention provides the important advantage that the redistributionchamber, in particular the wall part with bore holes, that is on bothsides exposed to corrosive carbamate-containing solution, can in anembodiment be made of (and consist of) single sheet corrosion resistantsteel, such as single sheet duplex stainless steel. This is inparticular the case when the condensation is on the shell side.Multi-layered walls of the chamber are also possible, especially if alllayers are of corrosion-resistant material. In some embodiments, thethickness of the wall part with bore holes for the tubes is 0.5-2 timesthe thickness of any other part of the wall of the redistributionchamber, the wall part with bore holes being a flat plate. For instance,if the other parts of the redistribution chamber have walls of 1-2 cmthickness, the wall part with the bore holes for the tubes has athickness of 0.5-4 cm. In some embodiments, the thickness of the wallpart with bore holes for the tubes is 0.9-1.1 times the thickness of theother parts of the wall of the redistribution chamber. An advantage ofthe invention is that the wall part with the bore holes for tubes doesnot need to be a very thick plate such as in the case of a tube-sheet.

In an example embodiment, the condenser comprises two U-shaped tubebundles arranged with, in vertical direction, ABBA, wherein A is astraight part of the first tube bundle and B is a straight part of thesecond tube bundle, or wherein A is a straight part of the second tubebundle (in operation used e.g. for carbamate dissociation) and B is astraight part of the first tube bundle (in operation used e.g. forraising steam), and preferably with a vertical stack of fourredistribution chambers connected to the two tube bundles. In suchembodiment, the bends of the U-shaped tube bundle can be arranged inconcentric fashion (in particular in cross-section in the length-heightplane). Alternatively, the arrangement can be AABB which would give e.g.two sets of bends, within each tube bundle concentric and the two setsarranged above each other.

In a preferred embodiment of the urea production plant of the invention,the high pressure carbamate condenser comprises a tube bundle that isconnected through a redistribution chamber and a duct to a feed line.The feed line is used for feeding urea solution that also containscarbamate to the tubes of the tube bundle. The feed line is connected tothe stripper for receiving stripped urea solution from the stripperand/or is connected to the reactor for receiving a part of the ureasolution from the reactor. In a preferred embodiment, the feed linecomprises an expansion device and preferably a gas/liquid separator forseparating gas from the expanded urea solution. Preferably the feed lineis configured for supplying at least a part of the expanded ureasolution to the duct.

In a preferred embodiment, the tube bundle (receiving urea solution alsocomprising carbamate) is connected through an outlet redistributionchamber and a duct to a gas/liquid separator. The gas/liquid separatorpreferably has a liquid flow connection to a recovery section and a gasflow connection to a second condenser. The ammonia and CO₂ obtained bythermal dissociation of carbamate in the tubes, is condensed at leastpartially in the second condenser. Preferably the second condenseroperates at medium pressure. Preferably the condensation is carried outin heat exchanging contact with an evaporation section of the ureaplant, such that the heat of condensation is used for evaporation ofwater from a urea solution. Preferably the second condenser has a liquidflow connection for a carbamate recycle stream to the high pressurecarbamate condenser, and more preferably to the shell space.

The HP condenser may in addition comprise a second tube bundle connectedto a feed line for process condensate (i.e. water) and connected to adrain line for steam.

In a preferred embodiment, the condenser comprises one or more pairs ofthe ducts, each pair including an inlet duct and an outlet duct. Thecondenser preferably comprises one or more pairs of the redistributionchambers, each pair including an inlet redistribution chamber fordistributing cooling fluid feed from the inlet duct to a plurality oftubes and an outlet redistribution chamber for combining heated coolingfluid from a plurality of tubes to the outlet duct. For each pair theredistribution chambers are typically arranged at the same side of thestraight tube parts, in case of a U-shaped tube bundle, or at opposedsides (in length direction) of the tubes in case of straight tubebundle.

In a preferred embodiment, the redistribution chamber comprises aplurality of elements (such as plate elements) and is hence notcompletely unitary. These elements together provide the wall of theredistribution chamber. At least one of the elements is provided withbore holes for the tube, and the same or another element (e.g. otherplate) is provided with a hole for a duct. Preferably, at least oneother element is openable and closable, e.g. removable, therebyproviding access to the inside of the redistribution chamber. Theelement is for instance a cover plate. This element can be used formaking the inside of the redistribution chamber accessible, e.g. forhumans and/or for devices. In this way the inside of the redistributionchamber, i.e. the space for receiving the fluid, is accessible formaintenance and inspection of the redistribution chamber inside and thetubes, in particular for inspection of the tubes insides and forplugging of tubes. The plugging of tubes can involve placing a plug in atube at a tube end connected to a redistribution chamber. In a preferredembodiment, the redistribution chamber comprises fasteners for fasteningthe openable element to at least one other element, such as bolts. Forinstance, a box shaped redistribution chamber having an openable frontplate may comprise a front plate having openings and side plates withrecesses (e.g. a threaded hole) aligned with the openings. The openingsand recesses can receive a fastener such as a bolt.

The redistribution chamber may furthermore comprise spacers for spacingwall parts (e.g. plate elements) from each other, e.g. to provideresistance against compression forces.

The vessel preferably comprises supports for the redistribution chamber,for instance arranged below the redistribution chamber and on the shell.For example support elements can be provided below (and e.g. at the sameposition in the length direction of the vessel as) the wall partprovided with bore holes. The support may comprise a recess forreceiving a lug of a redistribution chamber for locking theredistribution chamber in place. The redistribution chamber or e.g. astack of redistribution chambers are e.g. provided with fixation meansfor holding the chambers in place in the shell.

Preferably, the surface area of the transversal cross-section of aredistribution chamber (cross section perpendicular to the length axisof the vessel) is less than 90% or less than 80% or less than 40% of thesurface area of the cross-section of the vessel (in particular, of thesurface area enclosed by the shell in that cross-section).

In case of a (vertical) stack of redistribution chambers, the surfacearea of the cross-section of the stack in the width-height plane(perpendicular to the central length axis of the vessel) is e.g. lessthan 90% or less than 80% or less than 70% of the surface area of thecross-section of the vessel (in particular, of the surface area enclosedby the shell in that cross-section).

Preferably, the shell space is a single undivided space wherein allparts of the space are in fluid communication with each other; also insuch embodiments the shell space can include baffles to divide the shellspace in compartments which are not completely sealed off from eachother. Preferably the shell is in contact with the shell space, andpreferably the entire inner surface of the shell is in contact with theshell space. Preferably each duct extends through the shell space.Preferably each duct comprises a length segment wherein the entireoutside wall of the duct is exposed to the shell space. Preferably thefront plate of a (or each) box shaped redistribution chamber (with holesfor connecting with tubes in an opposite back plate) is on the outsideside exposed to the shell space.

In some embodiments, at least one redistribution chamber is in operationat least partly submerged in condensed liquid, preferably eachredistribution chamber is at least partially submerged in condensedliquid and preferably at least one redistribution chamber is entirelysubmerged in condensed liquid, wherein the condensed liquid is condensedin the shell space.

In a preferred embodiment, the shell comprises an essentiallycylindrical middle part and two cap parts. Each cap part may comprise aplurality of shell parts. A cap part is for instance a substantiallyhemispherical part, optionally with a manhole and plate. The two capparts close the middle part at opposed ends, in particular at opposedends in the length direction. Preferably the shell space is a singleshell space defined by the middle part and cap parts. Preferably theshell space is not divided, e.g. by dividing walls; yet can includebaffles. Preferably fluid can flow from the gas distributor to both ofthe cap parts.

High pressure carbamate condensers are different from other types ofheat exchangers, in particular hot gas coolers, by a number of features,which are preferred for the inventive carbamate condenser. A horizontalcarbamate condenser configured for condensation in the shell may forinstance include baffles (or partitions), which divide the shell spacein compartments in the length direction and which extend from the bottomof the vessel, but not entirely to the top thereby leave a gas dischargearea at the top of the shell; the top of the baffles define the liquidlevel of the condensate in operation. Some of the baffles can haveopenings e.g. at the vertical height of the tube bundle. Typically, themost downstream baffle has no opening in it, such that liquid condensateflows over the baffle top to the liquid outlet in the shell. Hence, theshell section comprises a weir. This allows for control of the level ofthe condensate in the condenser, especially to completely submerge thetube bundle. Furthermore typically the tube bundle, especially U-shapedtube bundle, has a once-through configuration or each cooling fluid(urea solution and/or process condensate).

A carbamate condenser with condensation in the tubes, e.g. of thehorizontal kettle type, comprises for example an ejector at the inlet ofthe carbamate solution, and for instance comprises a mixing zone forinlet of gas to be condensed and carbamate solution. The carbamatecondenser has for instance a conduit for recycle carbamate solution froman outlet end of a tube to an inlet for gas to be condensed.

In case of a vertical carbamate condenser which is configured forcondensation in the shell space, the condenser comprises for instance apacked part at the top, e.g. a part with a packing for scrubbing off-gaswith a solution supplied through an inlet of the shell above the packedpart, in particular an inlet for carbamate solution, and a down pipearranged below the packed part but above the U-bend of the tube bundleto a part of the condenser below said bend. The vertical carbamatecondenser preferably has an outlet for liquid of the shell, optionallywith a down pipe, such that in operation a liquid level is maintainedabove the U-bend of the tube bundles, wherein tube ends are at thebottom of the vessel.

The ducts preferably comprise, or are made of, a corrosion resistantsteel, such as a duplex stainless steel. For instance the ducts are madeentirely of such steel. The wall parts of the redistribution chambers,and any internal structures such as spacers that are in operation incontact with carbamate, are preferably made of corrosion resistantsteel, such as duplex stainless steel. The tubes, and the preferredinternal lining of the shell, are preferably made of corrosion resistantsteel, such as duplex stainless steel.

Suitable duplex stainless steel for said parts of the carbamatecondenser include for example the steel available as Safurex® steel andhaving composition 29Cr-6.5Ni-2Mo—N, which is also designated by ASMECode 2295-3 and by UNS S32906, or e.g. steel available as DP28W™ steeland having composition 27Cr-7.6Ni-1 Mo-2.3W—N, which is also designatedby ASME Code 2496-1 and by UNS S32808. Safurex® steel has for instancethe composition (% by mass): C: max. 0.05, Si: max. 0.8, Mn: 0.3-4.0,Cr: 28-35, Ni: 3-10, Mo: 1.0-4.0, N: 0.2-0.6, Cu: max. 1.0 W: max. 2.0S: max. 0.01 Ce: 0-0.2, balance Fe and (unavoidable) impurities.Preferably the ferrite content is 30-70% by volume and more preferably30-55%. More preferably, the steel contains (% by weight): C max. 0.02,max. 0.5 Si, Cr 29 to 33, Mo 1.0 to 2.0, N 0.36 to 0.55, Mn 0.3 to 1.0,balance Fe and impurities. Also suitable is a duplex stainless steelhaving the composition weight % (wt %): C max 0.030; Si max 0.8; Mn max2.0; Cr 29.0 to 31.0; Ni 5.0 to 9.0; Mo less than 4.0; W less than 4.0;N 0.25-0.45; Cu max 2.0; S max 0.02; P max 0.03; balance Fe andunavoidable occurring impurities; and wherein the content of Mo+W isgreater than 3.0 but less than 5.0 (wt. %), furthermore preferably witha steel composition as described in WO 2017/014632 hereby incorporatedby reference. In some embodiments the shell comprises an internal liningmade of such steels.

Each duct has a first duct end connected with a wall of theredistribution chamber and a second end connected with the shell. Thefirst duct end is aligned with an opening in the wall and the secondduct end is aligned with an opening in the shell, such that fluid canflow from outside the shell to the redistribution chamber through theduct. The duct is at least in part located in the vessel. The first ductend is located in the vessel. The duct extends through the vessel space.Furthermore, the outer surface of the duct is exposed to the shellspace.

The duct may consist of one or more duct parts, e.g. duct parts arrangedin series and connected with each other.

The first duct end is connected to a redistribution chamber, e.g. with aweld. The first duct end is for example placed radially outwardly of thetube ends connected to that redistribution chamber, i.e. further removedfrom the central length axis of the vessel in a direction perpendicularto the length. In an example embodiment with a box-shaped redistributionchamber with a bottom, top, front, back and two side plates, the ductend is for instance attached to a side, top or bottom plate, and thetube ends are attached to the back plate and the front plate is e.g. acover plate that can be opened for maintenance and inspection. Inprinciple, the duct can also be connected to the back plate or to thefront plate. In an example embodiment with a box shaped redistributionchamber, a duct is connected to the front plate and a side plate can beopened.

In a preferred embodiment a plurality of redistribution chambers arestacked on each other, to give a stack, preferably of box-shapedredistribution chambers and preferably a vertical stack. Preferably aplate element is common to the stacked redistribution chambers,preferably a plate element with bore holes.

Preferably the tube bundle contains U-shaped tubes wherein each tube hasa bend and two legs. Preferably the stack of redistribution chambersincludes an inlet redistribution chamber and an outlet redistributionchamber connected to the same U-shaped tube bundle.

In case of a (vertical) stack of preferably box-shaped redistributionchambers, various plates can be common to the redistribution chambers ofthe stack, this can be the case e.g. for a back plate (e.g. with boreholes for connecting with a tube bundle) and for a side plate. Ahorizontal plate can be common to two adjacent chambers, providing a topplate and a bottom plate, in particular when the chambers receivingfluid at the same pressure in operation. In case of a vertical stack offour or more redistribution chambers, for the top redistribution chambera duct can be connected to a top plate, for a bottom redistributionchamber a duct can be connected to a bottom plate, and for theredistribution chambers in the middle ducts can be connected to a sideplate. In a preferred embodiment, a redistribution chamber is providedwith ducts at two opposed side plates, and these are in operation forexample used both as inlet or both as outlet. This may advantageouslycontribute to good distribution of fluid over the tubes and efficientremoval of fluid from the tubes. In particular because in someembodiments a box shaped redistribution chamber has a width (from sideto side) that is longer than the height of the redistribution chamber,and wherein the same applies for the area of the back plate that isprovided with holes.

In an example embodiment with a stack of redistribution chambers, allducts connected to that stack extend to the top of the shell. Incombination with e.g. support structures for the tube bundle in thevessel between the shell bottom and the tube bundle, this may allow foradapting to expansion and/or contraction of the equipment. In case of astack of redistribution chambers, the chambers may have e.g. a commonshared back plate, and for a vertical stack also common shared sideplates.

In some example embodiments, the spacing in the length direction betweena first and second end of a duct is for one or more ducts (or even forall ducts) less than 20% or less than 10% of the length of the vessel,or less than 20% or less than 10% of the length of the straight parts ofthe tubes.

In a further embodiment, one or more ducts extend in the lengthdirection, for example with the ducts arranged substantially parallel(e.g. less than 5° deviation) with the (straight parts) of the tubes. Insome example embodiments, the spacing in the length direction between afirst and second end of a duct is for one or more or even all ducts,more than 10% or more than 20% of the length of the straight parts ofthe tubes.

Generally, for a redistribution chamber, the number of tubes connectedto that redistribution chamber is at least 10 times higher than thenumber of ducts connected to that redistribution chamber, e.g. at least50 times or at least 100 times higher. Accordingly, the ducts generallyhave a surface area in transversal cross section (perpendicular to theflow direction) of the internal flow space of the duct that is at least10 or at least 20 times larger than that of a tube.

Each duct has at least two duct ends, wherein duct ends refers to endparts and not only to the side edge. A duct may also have e.g. threeduct ends in case of a Y-shaped duct. A duct ends is connected to theredistribution chamber. For instance, a duct edge may be adjoined to a(planar) side of a redistribution chamber wall with a crevice-freejoint. A duct end may also be inserted through an opening in aredistribution chamber wall, for instance with the crevice between thewall and duct part being sealed off by a weld.

In the same way, a duct end (end part) is connected with the shell, e.g.a duct end may be adjoined to the shell, for instance with a crevicefree joint. In case the shell wall includes a carbon steel element andthe fluid to be transported through the duct includes carbamate, theduct end or a part of the duct can be inserted through an opening in theshell. A crevice between the inserted duct part and the hole surface ofthe shell (including any exposed carbon steel) can be closed off bywelding also at the inner side of the shell as the well place will beaccessible. Optionally, a duct part such as a sleeve (e.g. of duplexstainless steel) is first inserted through a hole, the crevice is sealedoff e.g. by welding, and the inserted duct part (e.g. sleeve) isconnected to another duct part e.g. by internal bore welding. Forinstance the condenser comprises a duct end part inserted through anopening in the shell and having a sealed crevice between the insertedduct part and the shell.

In an embodiment wherein a redistribution chamber is provided with aplurality of ducts, these ducts are optionally connected to a header (orjoint segment) which can be placed inside or outside the vessel. In someembodiments, the duct comprises a joint segment (e.g. T-joint) whichconnects at least three duct segments. With such a duct, two duct endscan e.g. be connected to the redistribution chamber and one duct end tothe shell. In an example embodiment, an inlet duct is connected to abottom plate of a bottom redistribution chamber of a vertical stack ofredistribution chambers by two or more duct segments each connected tothe bottom plate, at least one duct segment connected to the shell, anda joint segment located inside the vessel space joining the ductsegments. The at least two duct segments connected to the redistributionchamber can be spaced apart from each other for optimally distributingfluids over the tubes.

The condenser can be constructed for example with a method comprisingmounting a tube bundle in the shell (having at least one open end), suchas on support baffles. The invention also pertains to such aconstruction method. The method can comprise connecting theredistribution chambers to the tube ends before or after mounting thetube bundle, e.g. using internal bore welds. For instance a tube bundleconnected to a stack of redistribution chambers is mounted in the shell.The method may involve connecting the ducts to the redistributionchamber after mounting the tube bundle. The ducts can be insertedthrough the shell before or after the mounting. The method may involveclosing the vessel by e.g. joining a closing cap (e.g. a hemi-head) toan essentially cylindrical middle part of the vessel having at least oneopen end, e.g. at the middle part end where the redistribution chamberis located.

Example embodiments of the invention are illustrated and discussed inconnection with the drawings, these drawings do not limit the inventionor the claims.

FIG. 1 shows a reference high pressure carbamate condenser not accordingto the invention. The condenser (100) is provided as a shell-and-tubeheat exchanger (101) and is configured as a horizontal submergedcondenser with a U-shaped tube bundle (103) for cooling fluid and havingin operation the gas to be condensed in the shell space (105). A part ofthe bottom half of the condenser (100) is shown in FIG. 1. The heatexchanger (101) comprises a vessel (102), the vessel comprises a shell(1) and a tube bundle (103). The shell is designed to withstand highpressure and encloses a vessel space (104). The vessel (102) alsocomprises a header (107). The header (107) is not enclosed by the shell(1) and is outside the vessel space (104). The tubes (2) of the tubebundle (103) are provided in the vessel space (104). The space betweenthe tubes (2) and the shell (1) is the shell space (105) for receivinggas to be condensed. Accordingly, the vessel comprises a gas inlet (4)to the shell space (105), and an outlet (5) for liquid from the shellspace (104), and respective openings for process medium in the shell(1). The vessel furthermore comprises a carbamate recycle inlet (13)comprising an opening in the shell (1). The vessel further contains agas distributor (6) that is connected to the gas inlet (4). The gasdistributor (6) is configured for distributing the gas to be condensed(e.g. mixed gas from a high pressure stripper of a urea plant) in theshell space (105).

The vessel (102) further comprises a tube sheet (108). The tube sheetseparates the shell space (105) from the header (107) and thereforeneeds to withstand large pressure differences. One open end of theessentially cylindrical shell (1) is sealed off by the tube sheet (108).The tube sheet contains bore holes (110) for cooling fluid. The ends (3)of the tubes (2) are connected to the tube sheet (108), such that fluidcan flow between the tubes and the header (107). The header is providedwith an opening (109) that is used as inlet or outlet, such that coolingfluid flows between the opening (109) to a large number of tubes (2),e.g. more than 100 tubes. The tube sheet (108) is for instance anessentially circular metal plate and is typically a thick carbon steelplate (e.g. about 30 to 60 cm carbon steel) lined with corrosionresistant steel on the side exposed to the shell space (105), such aswith a duplex stainless steel alloy lining (which includes e.g. a weldoverlay).

For the reference carbamate condenser of FIG. 1 (not according to theinvention), the construction of the tube sheet (108) is challenging andexpensive, in view of the need to withstand high pressure, the exposureof at least one side to the very corrosive process medium, and the verylarge number of tubes. Furthermore any crevices between the tubes andtube sheet introduce a high risk of crevice corrosion because they arein contact with carbamate containing medium. Crevices are present forinstance in case of tube legs extending through the bore holes, e.g.with a bore diameters (slightly) larger than the outer diameter of thetube. Crevice corrosion is particularly severe for metal parts incontact with carbamate. Crevice corrosion can refer to the difficulty ofmaintaining a passivation layer on the steel with passivation agents(such as oxygen) in crevices due to the restricted flow in crevices.Corrosion also occurs in crevices if carbon steel is exposed in suchcrevices. Therefore in known pool condensers the tubes are frequentlynot inserted into the bores, but are joined to the tube sheet in acrevice free manner using e.g. internal bore welding. The exposure ofthe carbon steel part of the tube sheet to process condensate and steamin the bores is not problematic.

In case that a urea solution which also contains carbamate is providedas cooling fluid into header (107), such as when used for a process asdescribed in US 2015/0119603, a corrosion protective layer is alsonecessary on the side of tube sheet (108) exposed to the header (107),and the carbon steel surface of the bore holes (110) should not beexposed to the cooling fluid. The alternative of a single sheet duplexstainless steel alloy tube sheet is not practically feasible, becausehomogenous duplex stainless steel plates having a thickness (e.g. 30 to60 cm) sufficient to contain the high pressure medium are not feasibleto manufacture, at least in a practically acceptable way.

In US 2015/0086440 a construction method is described wherein sleevesare inserted in bore holes through the tube sheet such that the sleevesextend through the tube sheet. The sleeves are much shorter than thetubes. The sleeves can be (externally) welded on both sides of the tubesheet, such that the carbon steel layer of the tube shield is sealed offfrom the fluid in the shell space (105) and from fluid in the header(107). At one side of the tube sheet, the sleeves are subsequentlyconnected with the legs of the U-shaped tube bundle with an internalbore weld. Hence, after welding the sleeves to the tube sheet, the tubeends are connected to the sleeves by welding from the inside byinserting the welding probe in the sleeves from the low pressure side(header side) and forming an internal bore weld.

Accordingly, the external welding of the sleeves to the tube sheet iscarried out prior to connection of the sleeves to the tube bundle,because otherwise the tube bundle (with a large number of closely spacedtubes) prevents access at one side of the tube sheet. However, adisadvantage is that for each tube three welds are necessary, causinghigh construction costs.

If in the method of US 2015/0086440 the sleeve would be omitted and thetubes were directly connected to the tube sheet with internal borewelding, the carbon steel plate inside the tube sheet would exposed atthe bore holes to the carbamate present in the urea solution used ascooling fluid inside the tubes. This would induce corrosion. If thetubes were inserted into the bore holes, a crevice would be presentbetween the tube ends inserted in the bore holes and the tube sheet,i.e. a gap between the outside of the tube and the inside of thetube-sheet hole, allowing process medium to contact the carbon steelpart of the tube sheet. In the present invention the wall of theredistribution chamber (including the wall part with bore holes as in aconventional tube sheet) can advantageously be made of single sheetduplex stainless steel, such that an urea solution containing carbamatewhich is used as cooling fluid can be contacted with the surface of thebore holes without inducing excessive risk of corrosion.

In order to have a longer residence time of the condensate in the shellspace in the condenser of FIG. 1, one option is increasing the diameterof the shell, such that the shell has much larger surface area in crosssection than the tube bundle, e.g. as illustrated in U.S. Pat. No.5,767,313. A disadvantage is that the diameter of the tube sheet alsoincreases, because the tube sheet is used for sealing off one end of theshell, and hence the stress induced by the pressure differences alsoincreases.

FIG. 2A illustrates an example of a carbamate condenser (100) accordingto the invention. FIG. 2B shows an enlarged part. Instead of a header(107) and a tube sheet (108) as in FIG. 1, the carbamate condenser (100)contains a redistribution chamber (7) with a wall (8). The wall (8) isconfigured for separating fluid in the redistribution chamber (7) fromfluid in the shell space (105). These two fluids generally have adifferent composition in operation. The redistribution chamber (7) isprovided inside the vessel space (104) and is therefore enclosed by theshell (1). The shell (1) is configured for holding fluid that is influid contact with the outer surface of the tubes (2). A plurality oftubes (2 a, 2 b) are connected to each single redistribution chamber(7), such that fluid can flow between the tubes (2) and theredistribution chamber (7), through openings (12) (e.g. bore holes) inthe wall (8) that are provided in a part (11) of the wall (8). The ends(3) of the tubes (2) are attached to the wall (8) such that an openingsof the tube end is aligned with an opening (12) of the wall (8). This isschematically illustrated in FIG. 2C, with the diameter of the tubes (2a, 2 b) enlarged compared to the redistribution chamber (7). Theattachment of the tube end (3) is e.g. with an internal bore weld. Theredistribution chamber (7) is connected to an opening (10) in the shell(1) for (cooling) fluid by a duct (9). The duct (9) is placed in thevessel space (104) and is preferably exposed to the shell space (105).The duct (9) extends between the opening (10) of the shell (1) and theredistribution chamber (7), more in particular to an opening (14) of theredistribution chamber (7). In this way, cooling fluid can betransported between the opening (10) in the shell (1) and the tubes (2)through the redistribution chamber (7) and the duct (9) while thecooling fluid is separated from process medium fluid in the shell space(105). In operation, the duct (9) is on the inside in contact withcooling fluid and on the outside in contact with process medium in theshell space (105). As illustrated in FIGS. 2A and 2B, the carbamatecondenser (100) also contains a manhole (106) and baffles (15).

FIG. 2D schematically illustrates a cross section view perpendicular tothe length of an example embodiment. The carbamate condenser (100)comprises vertical stack of 4 box-shaped redistribution chambers (7)each having a duct (9), the part (11) with bore holes is indicated ineach redistribution chamber (7). The arrangement of the ducts (9) inFIG. 2D is schematic, numerous variations are possible. The ducts (9)generally extend from the redistribution chambers outwardly to anopening (1) in the shell (1). Reference numbers which are the same forFIGS. 1 and 2 preferably have the same features in FIG. 2 as describedin connection with FIG. 1.

FIG. 3 illustrates an example urea plant according to the invention. Theplant comprises a high pressure synthesis section comprising a ureareactor R, a stripper S, and a HP carbamate condenser HPCC. The reactorR has a liquid flow connection for urea synthesis solution USS to thestripper S which uses CO₂ feed for stripping, in addition to heating byindirect heat exchange with steam. Optionally, reactor R is combinedwith the condenser HPCC in a single vessel having a liquid flowconnection to the stripper S. The urea synthesis solution USS alsocontains carbamate, ammonia and water, which are to be removed (at leastin part) from the final urea product using the stripper S and a recoverysection REC comprising a low pressure section and e.g. consisting of alow pressure section without medium pressure section. Downstream of RECoptionally an evaporation section EVAP is provided for water removal togive a urea melt UM that is optionally solidified in a finishing sectionFINISH to give solid urea product SU. The stripper S has a gasconnection for mixed gas SG to the condenser HPCC. The condenser HPCCcomprises two U-shaped tube bundles T1 and T2. Each tube bundle (T1, T2)comprises numerous tubes (e.g. more than 100 tubes). Each tube isconnected with one end to a inlet redistribution chamber RC1A, RC2A andwith the other end to an outlet redistribution chamber RC1B, RC2B. Theinlet redistribution chamber (RC1A, RC2A) is connected to an inlet ductD1 a, D2 a. The outlet redistribution chamber (RC1B, RC2B) is connectedto an outlet duct (D1 b, D2 b).

Condensation is carried out on the shell side of HPCC, to which also theNH₃ feed is supplied. The stripper S has a liquid flow connection forstripped urea solution SUSS through an expansion device (e.g. expansionvalve) V1 to a flash vessel F1 for gas/liquid separation. Flash vesselF1 has a liquid connection for medium pressure urea solution MPUS whichstill contains carbamate to tube bundle T2. In tube bundle T2, the MPUSsolution is heated and carbamate in MPUS accordingly decomposes. Fromthe outlet of tube bundle T2, the MPUS solution is sent to a gas/liquidseparator, e.g. a flash vessel (F2). The gas G1 is sent to a condenserMPC typically operating at medium pressure (MP) and in heat exchangee.g. with the evaporation section EVAP. The liquid US1 from separator F2is sent to e.g. a low pressure recovery section (REC) for furtherremoval of carbamate and water, and then as urea solution US2 to theevaporation section EVAP. In the recovery section REC, the urea solutionis subjected to dissociation of carbamate by heating typically at lowpressure, the removed gases are condensed into liquid carbamate recyclestream CR2. The condenser MPC may also receive the gas G2 from flashvessel F1, and non-condensed gases G3 from HPCC and (not shown) off-gasfrom R. The condensate from MPC is sent using a pump (not shown) asliquid carbamate recycle CR1 to the synthesis section, in particular tothe shell space of the HPCC condenser, usually combined with a liquidcarbamate recycle (CR2) from a recovery section REC. The condenser HPCChas a liquid flow connection for condensate C to the reactor.Alternatively or in addition, a part of USS can be sent from R to tubebundle T2, e.g. to F, bypassing the stripper S. In tube bundle T1 water(typically condensate) is transformed into steam (not shown).

As used herein “a” and “an” includes one or more. The term “comprising”allows for the presence of other elements than those recited. Variousillustrative embodiments have been described above, in part withreference to the accompanying drawings, but the invention is not limitedto these embodiments. Features of the separately described embodimentscan generally be combined with each other as will be clear for theskilled person. Steps of the production processes can be implementedwith corresponding units and fluid flow connections of the inventiveplant. The process of the invention preferably is carried out in a plantas described and using the high pressure carbamate condenser asdescribed with all preferred device features applying equally for theprocess. Reference signs in the claims to the drawings provide exampleillustrations only and do not limit the claims.

The invention claimed is:
 1. A shell-and-tube heat exchanger whichcomprises a vessel which comprises a shell and at least one tube bundle,wherein the shell encloses a vessel space, wherein the tube bundlecomprises tubes having ends, and wherein a shell space is providedbetween the tubes and the shell, wherein the heat exchanger furthercomprises a redistribution chamber located in said vessel space, whereinsaid redistribution chamber comprises a wall for separating a firstfluid in the shell space from a second fluid inside the redistributionchamber, wherein the wall of the redistribution chamber comprises a flatplate comprising a plurality of bore holes, wherein a plurality of saidtubes are connected to a single redistribution chamber at said boreholes such that said second fluid can flow between said tubes and saidredistribution chamber, wherein the heat exchanger further comprises aduct extending from an opening for the second fluid in said shellthrough said vessel space to said redistribution chamber such that thesecond fluid can flow between a tube end and said opening for the secondfluid in said shell through said redistribution chamber and said duct.2. The heat exchanger according to claim 1, wherein the duct has a firstduct end connected with a wall of the redistribution chamber and asecond end connected with the shell.
 3. The heat exchanger according toclaim 2, wherein the first duct end is aligned with an opening in thewall and the second duct end is aligned with an opening in the shell,such that fluid can flow from outside the shell to the redistributionchamber through the duct; wherein the duct is at least in part locatedin the vessel; wherein the first duct end is located in the vessel;wherein the duct extends through the vessel space; and wherein the outersurface of the duct is exposed to the shell space.
 4. The heat exchangeraccording to claim 2, wherein the first duct end is connected to saidredistribution chamber.
 5. The heat exchanger according to claim 4,wherein the first duct end is connected to said redistribution chamberwith a weld.
 6. The heat exchanger according to claim 4, wherein thefirst duct end is placed radially outwardly of the tube ends connectedto that redistribution chamber.
 7. The heat exchanger according to claim1, wherein the duct has an outer surface exposed to the shell space. 8.The heat exchanger according to claim 1 configured for condensation of acompound.
 9. The heat exchanger according to claim 8, wherein thecompound is carbamate.
 10. The heat exchanger according to claim 1configured for operation at pressures below 100 bar.
 11. The heatexchanger according to claim 1, wherein the flat plate has a thicknessthat is 0.5 to 2 times the thickness of any other part of the wall ofthe redistribution chamber.
 12. The heat exchanger according to claim 1,wherein the redistribution chamber comprises an internal load bearingstructure.
 13. The heat exchanger according to claim 1, wherein theinternal load bearing structure is a spacer.